Supported carbon-containing molybdenum and tungsten sulfide catalysts, their preparation and use

ABSTRACT

A supported carbon-containing molybdenum sulfide and tungsten sulfide catalyst useful for conducting methanation and hydrotreating reactions, principally the latter, can be formed by compositing a preselected quantity of a porous, refractory inorganic oxide with a complex salt characterized by the formula 
     
         B.sub.x [MO.sub.y S.sub.4-y ] 
    
     where B is an organo or hydrocarbyl substituted diammonium ion, an organo or hydrocarbyl substituted ammonium ion or quaternary ammonium ion, or an ionic form of a cyclic amine containing one or more basic N atoms, x is 1 where B is an organo or hydrocarbyl substituted diammonium ion, or 2 where B is an organo or hydrocarbyl substituted ammonium or quaternary ammonium ion or an ionic form of a cyclic amine containing one or more basic N atoms, M is molybdenum or tungsten, and y is 0, or a fraction or whole number ranging up to 3, and heat decomposing the salt of said catalyst precursor composite in the presence of hydrogen, hydrocarbon and sulfur to form said supported carbon-containing molybdenum sulfide or tungsten sulfide catalyst.

BACKGROUND OF THE INVENTION

(1) Field of the Invention

This invention relates to a process for the preparation of supportedcarbon-containing molybdenum and tungsten sulfide catalysts, thesupported catalyst species prepared by such process, and to the use ofsuch catalysts in methanation or hydrotreating. In particular, itrelates to a process for the preparation of a species of highly active,highly selective supported, metal-promoted hydrotreating catalysts, thecatalyst species prepared by such process, and the use of such catalystspecies in conducting methanation and hydrotreating processes,particularly the latter.

(2) Background and Prior Art

Hydrotreating processes are basic, and very well known to the petroleumrefining industry. These processes require the treating with hydrogen ofvarious hydrocarbon fractions, or whole heavy feeds, or feedstocks, inthe presence of hydrogenation (hydrogen transfer) catalysts to effectconversion of at least a portion of the feeds, or feedstocks to lowermolecular weight hydrocarbons, or to effect the removal of unwantedcomponents, or compounds, or their conversion to innocuous or lessundesirable compounds. Hydrotreating may be applied to a variety offeedstocks, e.g., solvents, light, middle, or heavy distillate feeds andresidual feeds, or fuels. In hydrofining relatively light feeds, thefeeds are treated with hydrogen, often to improve odor, color,stability, combustion characteristics, and the like. Unsaturatedhydrocarbons are hydrogenated, and saturated. Sulfur and nitrogen areremoved in such treatments. In the treatment of catalytic crackingfeedstocks, the cracking quality of the feedstock is improved by thehydrogenation. Carbon yield is reduced, and gasoline yield is generallyincreased. In the hydrodesulfurization of heavier feedstocks, orresiduas, the sulfur compounds are hydrogenated and cracked.Carbon-sulfur bonds are broken, and the sulfur for the most part isconverted to hydrogen sulfide which is removed as a gas from theprocess. Hydrodenitrogenation, to some degree also generally accompanieshydrodesulfurization reactions. In the hydrodenitrogenation of heavierfeedstocks, or residuas, the nitrogen compounds are hydrogenated andcracked. Carbon-nitrogen bonds are broken, and the nitrogen is convertedto ammonia and evolved from the process. Hydrodesulfurization, to somedegree also generally accompanies hydrodenitrogenation reactions. In thehydrodesulfurization of relatively heavy feedstocks, emphasis is on theremoval of sulfur from the feedstock which is usually converted to lowermolecular weight, or lower boiling components. In thehydrodenitrogenation of relatively heavy feedstocks emphasis is on theremoval of nitrogen from the feedstock, which also is converted to lowermolecular weight, or lower boiling components. Albeit,hydrodesulfurization and hydrodenitrogenation reactions generally occurtogether, it is usually far more difficult to achieve effectivehydrodenitrogenation of feedstocks than hydrodesulfurization offeedstocks.

The dwindling supplies of high grade petroleum feedstocks necessitatesthe increased production and processing of transportation fuels fromlower grade, heavy petroleum feedstocks and synthetic liquidhydrocarbons derived from hydrocarbon-containing, or precursorhydrocarbon-containing, solids. The refiners' feedstock sources as aresult thereof continue to change, particularly as the worldwidesupplies of petroleum diminish. The newer feedstocks often containhigher amounts of nitrogen, sulfur, and other materials. Nonetheless,whatever the difficulties, it remains a necessity to effectivelyhydrotreat the new feedstocks; often to a greater extent than previouslywas required. It has thus become necessary to process whole heavypetroleum crudes and residua from unconventional sources, as well assynthetic fuels (syncrudes; e.g. liquified coal, oil from coalcarbonization, oil from tar sands, shale oil and the like inclusive ofresidua or viscous syncrude fractions). All, particularly the later, areunder active consideration as commercial feedstocks, or feedstockreplacements for higher grade petroleum sources. Feedstocks derived fromthese sources are often of high olefinic content, contain more sulfur ornitrogen, or both, than feedstocks derived from more conventional crudeoils.

Naphthas, notably those derived from syncrudes, viz. residua, shale oil,and coal, are highly unsaturated and contain considerably more sulfur,nitrogen, olefins, and condensed ring compounds than the moreconventional naphthas. For example, nitrogen and sulfur are contained incat naphtha in concentrations ranging upwardly from 50 ppm and 1000 ppm,respectively. In coal liquids nitrogen and sulfur are present inconcentrations ranging upwardly from 1300 ppm and 5000 ppm,respectively; and oxygen is presently in even higher concentrations.These compounds cause activity suppression and an all too rapiddeactivation of the catalysts. Coke formation is increased, and there ismore cracking with increased gas production. Albeit these compounds,except for condensed ring naphthenic compounds, can be removed byconventional hydrofining, this is a severe, if not an intolerableprocess burden due to the large hydrogen consumption; and hydrogenbecomes more and more a very expensive commodity. Thus, generallyconsiderably more upgrading is required to obtain usable products fromthese sources. Such upgrading generally necessitates hydrotreating thevarious hydrocarbon fractions, or whole crudes, and includes reactionssuch as hydrogenating to saturate olefins and aromatics,hydrodesulfurizing to remove sulfur compounds, hydrodenitrogenating toremove nitrogen, and conversion of high boiling compounds to lowerboiling compounds.

Typical hydrotreating catalysts are exemplified by cobalt molybdate onalumina, nickel molybdate on alumina, cobalt molybdate promoted withnickel, and the like. Certain transition metal sulfides such as cobaltand molybdenum sulfides and mixtures thereof have also been employed inhydrofining processes for upgrading oils which contain sulfur andnitrogen compounds. For example, U.S. Pat. No. 2,914,462 discloses theuse of molybdenum sulfide for hydrodesulfurizing gas oil and U.S. Pat.No. 3,148,135 discloses the use of molydenum sulfide for hydrorefiningsulfur and nitrogen-containing hydrocarbon oils. U.S. Pat. No. 2,715,603discloses the use of molybdenum sulfide as a catalyst for thehydrogenation of heavy oils, while U.S. Pat. No. 3,074,783 discloses theuse of molybdenum sulfides for producing sulfur-free hydrogen and carbondioxide, wherein the molybdenum sulfide converts carbonyl sulfide tohydrogen sulfide. A serious disadvantage associated with the use of suchcatalysts is their relatively high cost, and the supply of catalyticmetals is rather limited. Moreover, the reaction rates of such catalystsare relatively slow, particularly in the presence of nitrogen; andhydrogen consumption is quite high. These latter problems areparticularly oppressive when it is realized that new generation feedsare unusually high in nitrogen, or sulfur, or both, and the cost ofhydrogen is increasing at very high rates.

Molybdenum sulfide is also known to be useful for water gas shift andmethanation reactions, as well as for catalyzed hydrotreatingoperations. Recently, e.g., it was disclosed in U.S. Pat. Nos. 4,243,553and 4,243,554 that molybdenum disulfide catalysts of relatively highsurface area can be obtained by thermally decomposing selectedthiomolybdate salts at temperatures ranging from 300°-800° C. in thepresence of essentially inert, oxygen-free atmospheres, e.g.,atmospheres of reduced pressure, or atmospheres consisting of argon,nitrogen, and hydrogen, or mixtures thereof. In accordance with theformer, a substituted ammonium thiomolybdate salt is thermallydecomposed at a very slow heating rate of from about 0.5° to 2° C./min,and in accordance with the latter an ammonium thiomolybdate salt isdecomposed at a rate in excess of 15° C. per minute to form the highsulface area molybdenum disulfide.

There remains a need in the art for new, improved hydrotreatingcatalysts, especially hydrotreating catalysts which are more highlyactive, selective, and stable.

It is accordingly a primary objective of the present invention toprovide this need, particularly by providing new and improvedhydrotreating catalysts, a process for the preparation of thesecatalysts, and process for the use of these catalysts in conductinghydrotreating reactions.

A particular object is to provide novel hydrogen efficient hydrotreatingcatalysts which are especially active for the hydrodesulfurization, orhydrodenitrogenation, or both, of hydrocarbon feedstocks which containrelatively high concentrations of sulfur, or nitrogen, or both; as wellas a process for the use of such catalysts in conducting such reactions.

A further, and more particular object is to provide novel hydrotreatingcatalysts of such character which are highly selective for conductinghydrodesulfurization, or hydrodenitrogenation reactions, or both; aswell as a process for the use of such catalysts in conducting suchreactions.

A yet further, and more specific object is to provide novel methanationcatalysts, a process for the preparation of such catalysts, and aprocess for the use of such catalysts in conducting methanationreactions.

DESCRIPTION OF THE INVENTION

These and other objects are achieved in accordance with the presentinvention embodying catalysts, and process for producing such supportedcarbon-containing molybdenum and tungsten sulfide hydrotreatingcatalysts, both promoted and unpromoted species, which have admirablyhigh activity, selectivity, and stability especially in conductinghydrodesulfurization and hydrodenitrogenation reactions at high levelsof hydrogen efficiency with various sulfur and nitrogen containinghydrocarbon feeds. In accordance therewith, a supportedcarbon-containing molybdenum sulfide and tungsten sulfide hydrotreatingcatalyst is formed by compositing a preselected quantity of a porous,refractory inorganic oxide with a complex salt characterized by theformula

    B.sub.x [MO.sub.y S.sub.4-y ]

where B is an organo or hydrocarbyl substituted diammonium ion, anorgano or hydrocarbyl substituted ammonium ion or quaternary ammoniumion, or an ionic form of a cyclic amine containing one or more basic Natoms, x is 1 where B is an organo or hydrocarbyl substituted diammoniumion, or 2 where B is an organo or hydrocarbyl substituted ammonium orquaternary ammonium ion or an ionic form of a cyclic amine containingone or more basic N atoms, M is molybdenum or tungsten, and y is 0, or afraction or whole number ranging up to 3, and heat decomposing the saltof said catalyst precursor composite in the presence of hydrogen,hydrocarbon and sulfur to form said supported carbon-containingmolybdenum sulfide or tungsten sulfide hydrotreating catalyst. Suitably,a solution of the salt, or admixture of salts, is incorporated with apreselected quantity of a porous, refractory inorganic oxide support,preferably a particulate mass of said support, the salt-containingsupport then preferably dried to remove all or a portion of the solventfrom the support, and the dried particulate salt-containing support thenheated in the presence of hydrogen, hydrocarbon, and sulfur or asulfur-bearing compound to the decomposition temperature of said salt,or salts, to form the catalyst species of this invention. Suitably,sufficient of the salt, or salts, is incorporated on the support so thatprior to, or at the time the salt, or salts, is decomposed from about 5percent to about 30 percent, preferably from about 10 percent to about25 percent of the salt, expressed as weight MoO₃ or WO₃ on an ignitionloss free basis, will be present on the support. The supported catalystspecies is stable, highly active and selective as a hydrotreatingcatalyst. The hydrotreating capacity of such catalysts in a preferredembodiment can be further promoted, and transformed into a yet moreeffective hydrotreating catalyst by the incorporation therewith of aGroup VIII metal or admixture of such metals, of the Periodic Table ofthe Elements (E. H. Sargent & Co., Copyright 1962, Dyne-Slide Co.).

The precise nature, and composition of the catalyst species that isformed as a reaction product of the decomposition reaction is not known,but it is believed that a catalyst species having the general formulaMS_(2-z) C_(z'), wherein M is molybdenum or tungsten, and z and z' arethe same or different and range from about 0.01 to about 0.5, is formed,and supported upon the porous, refractory inorganic oxide base. Thesurface composition, or composition deposited on the surface of thesupport, is thus believed to correspond generally with the unsupportedcatalyst species defined in application Ser. Nos. 399,999 and 399,991,each jointly filed by Theresa R. Pecoraro and Russel R. Chianelli, andRussel R. Chianelli and Theresa R. Pecoraro, respectively, of even dateherewith; the disclosures of which are herewith incorporated byreference.

The catalyst species of Pecoraro and Chianelli are, like those ofApplicants, defined as carbon-containing molybdenum and tungstensulfides, useful for hydrorefining hydrocarbon feedstocks, and thesebasic materials can be promoted with transition metal sulfides such ascobalt sulfide. These catalyst species are preformed, or formed in-situ,by contacting a hydrocarbon feed at elevated temperature with one ormore catalyst precursors selected from the group consisting of (a)ammonium thiomolybdate or thiotungstate salts, (b) ammonium molybdate ortungsten salts, (c) substituted ammonium thiomolybdate or thiotungstatesalts, (d) substituted ammonium molybdate or tungstate salts, andmixtures thereof. Unlike Applicants' catalyst species, however, thecatalyst species of Pecoraro and Chianelli are unsupported, bulkcatalysts. They thus differ from the supported carbon-containingmolybdenum and tungsten catalyst species defined herein; and differsubstantially, inter alia, in that the catalyst species of the presentinvention achieves superior utilization of the catalytic metals presenton the catalyst, and better hydrogen utilization.

A starting material for use in the preparation of the catalyst of thisinvention can, as suggested, be characterized as an organo orhydrocarbyl diammonium ion substituted, an ammonium or quaternaryammonium ion substituted, or an ionic form of a basic cyclic aminesubstituted thiomolybdate, or thiotungstate, salt having the formulaB_(x) [MO_(y) S_(4-y) ], supra. In such formula B is thus an organo orhydrocarbyl substituted diammonium ion, an organo or hydrocarbylsubstituted ammonium ion or quaternary ammonium ion, or an ionic form ofa cyclic amine containing one or more basic N atoms, x is 1 where B isan organo or hydrocarbyl substituted diammonium ion, or 2 where B is asubstituted ammonium or quaternary ammonium ion, or an ionic form of acyclic amine containing one or more basic N atoms, M is molybdenum ortungsten, preferably molybdenum, and y is 0, or a fraction or wholenumber ranging up to 3. Preferably y ranges from 0 to 0.5. In theformula the B moiety, or moieties, constitutes a cationic entity, orentities, which forms a complex with an anionic [MO_(y) S_(4-y) ]²⁻moiety. An organo, or hydrocarbyl diammonium ion moiety thus providestwo positive charges in formation of a B_(x) [MO_(y) S_(4-y) ] salt. Onthe other hand, two of the substituted ammonium or quaternary ammoniumions, or anionic form of a cyclic amine which contains one or more basicN atoms complex with an anionic [MO_(y) S_(4-y) ]²⁻ moiety. Thesubstituent amino groups of the organo, substituted diammonium ion, orsubstituted ammonium ion, where B is a substituted diammonium ion orsubstituted ammonium ion, can be characterized as primary, secondary ortertiary, in that the hydrogen atoms of one or both of the substituentamino groups of B can be substituted or unsubstituted as with an organo,a hydrocarbyl radical or hydrocarbon radical selected from the groupconsisting of alkyl, aralkyl, cycloalkyl, aryl, alkaryl, alkenyl, andalkynyl, preferably alkyl or aryl, and including such radicals wheninertly substituted. Such radical can thus be exemplified by hydrocarbongroups which contain from about one to about 30 carbon atoms, preferablyfrom about one to about 20 carbon atoms. When the hydrocarbyl, orhydrocarbon radical is alkyl, it can typically be methyl, ethyl,n-propyl, iso-propyl, n-butyl, i-butyl, sec-butyl, amyl, octyl, decyl,octadecyl, and the like. When it is aralkyl it can typically be benzyl,betaphenylethyl, and the like. When it is cycloalkyl, it can typicallybe cyclopentyl, cyclohexyl, cycloheptyl, cyclooctyl,2-methyl-cycloheptyl, 3-butyl cyclohexyl, 3-methyl cyclohexyl, and thelike. When it is aryl, it can typically be phenyl, ethylphenyl, and thelike. When alkaryl, it can typically be tolyl, xylyl, and the like. Whenalkenyl, it can typically be vinyl, allyl, 1-butenyl, and the like. Whenit is alkynyl, it can typically be ethynyl, propynyl, butynyl, and thelike. The hydrocarbyl, or hydrocarbon radical can be inertlysubstituted, i.e., it may bear a non-reactive substituent such as alkyl,aryl, cycloalkyl, ether, halogen, nitro, and the like. Typically inertlysubstituted groups may include 3-chloropropyl, 2-ethoxyethyl,4-methylcyclohexyl, p-chlorophenyl, p-chloro benzyl,3-chloro-5-methylphenyl, and the like.

Exemplary of B, i.e., where B is a diammonium ion substitutient of suchsalts, are the ionic forms of aliphatic diamines; e.g., alkyl diaminessuch as those derived from straight chain hydrocarbons which contain anamino group on two different carbon atoms, as on each terminal carbonatom, i.e., H₂ N(CH₂)_(n) NH₂, where n ranges from 1 to about 30,preferably from 1 to about 20, illustrative of which are methyldiamines, ethylene diamines, n-propyl diamines, hexyl diamines, decyldiamines, dodecyl diamine, and the like, and including aliphaticdiamines which contain amino groups on adjacent carbon atoms such as 1,2bis(amino)-n-butane, or those which contain amino groups on separatedcarbon atoms such as 1,3 bis(amino)-n-butane, or the like; cyclicdiamines, e.g., aromatic diamines, such as those which contain twoprimary amino groups attached to a fused or non-fused ring structure,e.g., p-diamino benzene, phloroglucinol, o-diamino naphthalene,p-phenylene-diamines, and the like. Suitable salts formed from suchsubstitutients are thus exemplified by

[H₃ NC₃ H₆ NH₃ ][MoO₀.5 S₃.5 ];

[H₃ NC₆ H₁₂ NH₃ ][MoO₀.3 S₃.7 ];

[H₃ NC₈ H₁₆ NH₃ ][WO₀.5 S₃.5 ];

[CH₃ CHNH₃ CHNH₃ C₂ H₅ ][MoO₀.4 S₃.6 ];

[CH₃ CHNH₃ CH₂ CHNH₃ C₃ H₇ ][MoO₀.5 S₃.5 ];

[CH₂ CHNH₃ CH₂ CHNH₃ C₃ H₇ ][MoS₄ ];

and the like.

The B moieties of the substituted ammonium thiomolybdate, orthiotungstate salt can, as suggested, also be constituted of ammoniumions wherein one or more of the hydrogen atoms of the ions have beenreplaced by an organo, hydrocarbyl or hydrocarbon radical, selected fromthe group consisting of alkyl, aralkyl, cycloalkyl, aryl, alkaryl,alkenyl and alkynyl, including such radicals when inertly substituted.The hydrocarbon moiety is exemplified by hydrocarbon groups whichcontain from 1 to about 30 carbon atoms, preferably from about one toabout 20 carbon atoms. Exemplary of substitutients associated with, orsubstituted upon the ammonium or quaternary ammonium ion to form each ofthe two B constituents of the salt are, when the substituent is alkyl,methyl, ethyl, n-propyl, iso-propyl, n-butyl, i-butyl, sec-butyl, amyl,octyl, decyl, octadecyl, and the like; when the substituent is aralkyl,benzyl, betaphenylethyl, and the like; when the substituent iscycloalkyl, cyclopentyl, cyclohexyl, cycloheptyl, cyclooctyl,2-methylcycloheptyl, 3-butyl cyclohexyl, 3-methyl cyclohexyl, and thelike; when the substituent is aryl, phenyl, ethylphenyl, and the like;when the substituent is alkaryl, tolyl, xylyl, and the like; when thesubstituent is alkenyl, vinyl, allyl, 1-butenyl, and the like; when thesubstituent is alkynyl, ethynyl, propynyl, butynyl, and the like. Thesubstituent, as suggested, can be inertly substituted, i.e., it may beara non-reactive substitutent such as alkyl, aryl, cycloalkyl, ether,halogen, nitro, and the like. Typically inertly substituted groups mayinclude 3-chloropropyl, 2-ethoxyethyl, 4-methyl cyclohexyl,p-chlorophenyl, p-chloro benzyl, 3-chloro-5-methylphenyl, etc.Substituted ammonium ions of such types are thus those containing oneorgano or hydrocarbyl group, e.g., n-C₄ H₉ NH₃ ⁺, C₆ H₅ NH₃ ⁺, and thelike, those containing two organo or hydrocarbyl groups, e.g., (C₂ H₅)₂NH₂ ⁺, (C₆ H₅)₂ NH₂ ⁺, and the like, those containing three organo orhydrocarbyl groups, e.g., n-(C₆ H₁₃)₃ NH⁺, (C₆ H₅)₃ NH⁺, and the like;and those containing four organo or hydrocarbyl groups, e.g., (C₆ H₅CH₂)₄ N⁺, (C₆ H₅)₄ N⁺, and the like. Suitable salts useful in thepractice of this invention are thus exemplified by

H₃ NC₆ H₄ NH₃ [MoO₀.2 S₃.8 ];

[(C₂ H₅)NH₃ ⁺ ]₂ [MoO₀.4 S₃.6 ];

[(C₆ H₅)₂ NH₂ ⁺ ]₂ [MoO₀.4 S₃.6 ];

[(C₆ H₅)₂ NH₂ ⁺ ]₂ [MoO₀.1 S₃.9 ];

[(C₆ H₁₃)₃ NH⁺ ]₂ [MoO₀.2 S₃.8 ];

[(C₆ H₅)₄ N⁺ ]₂ [MoO₀.1 S₃.9 ];

[(C₆ H₁₃)₄ N⁺ ]₂ [MoS₄ ]; [(C₆ H₅)₄ N⁺ ]₂ [WS₄ ];

and the like.

The B moieties of the catalyst precursor salt can, as suggested, also beconstituted of an ionic form of a cyclic amine which contains one ormore basic nitrogen atoms within the ring, generally from one to aboutthree basic atoms in the total molecule. This class of compounds can beconstituted of rings having 5, 6, or more members, and can be monocyclicor polycyclic, fused or non-fused rings, non-substituted or inertlysubstituted, which contain from one to about 3 basic nitrogen atoms inthe total molecule. Exemplary of ionic forms of cyclic amines of thischaracter are the ionic forms of such monocyclic five membered rings aspyrrole, isopyrrole, pyrazole, 2-isoimidazole, 1,2,3-triazole and thelike; such monocyclic six membered rings as pyridine, pyridazine,pyrimidine, pyrazine, s-triazine and the like; and such fused ring,polyclic structures as indole, 1,5-pyrinidine, quinoline, naphthyridine,purine, acridine and the like. Suitable salts useful in the practice ofthis invention are thus exemplified by [C₅ H₅ NH]₂ [MoO₀.5 S₃.5 ]; [C₄H₄ N₂ H]₂ [MoO₀.5 S.sub. 3.5 ]; [C₄ H₄ N₂ H]₂ [WO₀.4 S₃.6 ]; [C₃ H₃ N₃H]₂ [MoO₀.2 S₃.8 ]; [C₈ H₈ N₂ H]₂ [MoO₀.4 S₃.6 ]; [C₁₃ H₁₃ NH]₂ [MoS₄ ]and the like.

The organo or hydrocarbyl diammonium ion substituted, ammonium orquaternary ammonium ion substituted, or ionic form of a basic cyclicamine substituted thiomolybdate, or thiotungstate, salt is preferablyimpregnated upon a porous, refractory, inorganic, inorganic oxidesupport, suitably by first dispersing or dissolving said salt, oradmixture of salts, in a suitable solvent, and then admixing orslurrying a preselected amount of the precursor thiomolybdate, orthiotungstate, salt solution with a preselected quantity of said supportmaterial in particulate form. Virtually, any solvent can be employedwhich is capable of dissolving the precursor thiomolybdate orthiotungstate salt, without adversely reacting therewith. Albeit, anaqueous solvent can be employed, non aqueous solvents are preferredbecause few of the organo or hydrocarbyl diammonium ion substituted,ammonium or quaternary ammonium ion substituted, or ionic form of basiccyclic amine substituted thiomolybdate, or thiotungstate, salts areadequately soluble in water. Suitable solvents for dissolving thesesalts are alcohols, ethers, ketones, paraffins, cycloparaffins andaromatic hydrocarbons, exemplary of which are methyl alcohol, ethylalcohol, n-propyl alcohol, isopropyl alcohol, n-butyl alcohol, isobutylalcohol, sec-butyl alcohol, t-butyl alcohol, ethyl ether,tetrahydrofuran, acetone, methyl ethyl ketone, hexane, heptane,cyclobutane, aromatic hydrocarbons, notably those having a singlebenzene nucleus, especially aromatic hydrocarbons containing from about6 to about 9 carbon atoms, e.g., benzene, toluene, xylene, n-propylbenzene, isopropyl benzene, and the like; and cycloparaffin hydrocarbonswhich contain from about 4 to about 9 carbon atoms, e.g., cyclobutane,cyclopentane, cyclohexane, cycloheptane, and the like. Preferredsolvents are alcohols, especially the low molecular weight simplealcohols, e.g., methyl alcohol, ethyl alcohol and the like; amines,e.g., butyl amine, ethylenediamine and the like; and ketones, e.g.,acetone, methylethyl ketone, and the like.

The organo or hydrocarbyl diammonium ion substituted, ammonium orquanternary ammonium ion substituted, or ionic form of a basic cyclicamine substituted thiomolybdate, or thiotungstate, salt is composited orotherwise intimately associated with the porous, inorganic oxide supportby various techniques known to the art, such as coprecipitation,impregnation or the like. The composite is preferably formed from asolution of the desired salt, or salts by impregnation of the support,typically via an "incipient wetness" technique which requires a minimumof solution so that the total solution with the preselected desiredamount of the catalyst precursor salt is adsorbed, initially or aftersome evaporation. Typically, a particulate porous refractory inorganicoxide, notably alumina, in the form of beads, pills, pellets, seivedparticles, extrudates, or the like in dry or solvated state is contactedwith a solution of the salt, or admixture of the salts, with the resultthat the salt solution is adsorbed into the particulate material in thedesired amount. The salt-containing particulate material can thereafterbe heated and dried at low temperature, with or without vacuumassistance, e.g., at temperatures ranging at or below the boilingtemperature of the solvent.

The preferred support is alumina, and the composite support can containfor example, one or more of alumina, bentonite, clay, diatomaceousearth, zeolite, silica, activated carbon, magnesia, zirconia, thoria,titania and the like, these latter with alumina, usually in a range ofabout 1 to 20 percent, based on the weight of the support. A preferredsupport for the practice of the present invention is one having asurface area of more than 50 m² /g, preferably from about 100 to about300 m² /g, a bulk density of about 0.3 to 1.0 g/ml, preferably about 0.4to 0.8 g/ml, an average pore volume of about 0.2 to 1.1 ml/g, preferablyabout 0.3 to 0.8 ml/g, and an average pore diameter of about 30 to 300Å.

The catalyst precursor material, or material formed by impregnation ofthe support with the organo or hydrocarbyl diammonium ion substituted,substituted ammonium or quaternary ammonium ion, or ionic form of abasic cyclic amine salt is preferably dried to remove all or a portionof the solvent, but it is never calcined after the salt is added to thesupport. The support is preferably dried at a temperature below about100° C., more preferably between about 50° C. and 80° C., in thepresence of nitrogen or oxygen, or both, at static or dynamicconditions, in air or under vacuum. The catalyst precursor material, ona dry basis, contains from about 5 percent to about 30 percent,preferably from about 10 percent to about 25 percent of the undecomposedorgano or hydrocarbyl diammonium ion substituted, ammonium or quaternaryammonium ion substituted, or ionic form of a basic cyclic aminesubstituted thiomolybdate, or thiotungstate, salt, expressed as weightMoO₃ or WO₃ on an ignition loss free basis.

The catalyst precursor is heated to the decomposition temperature of theimpregnating salt, and the salt decomposed in the presence of hydrogen,and a hydrocarbon and sulfur, or sulfur-bearing compound, to form thesupported catalyst species of this invention. The nature of thehydrocarbon is not critical, and can generally include any hydrocarboncompound, acyclic or cyclic, saturated or unsaturated, unsubstituted orinertly substituted hydrocarbon. The preferred hydrocarbons are thosewhich are liquid at ordinary temperatures, exemplary of which are suchstraight chain saturated acyclic hydrocarbons as octane, dodecane,hexadecane, or the like; straight chain unsaturated acyclic hydrocarbonsas 2-hexene, 1,4-hexadiene, and the like; branched chain saturatedacyclic hydrocarbons, as 3-methyl pentane, neopentane, isohexane,2,7,8-triethyl decane, and the like; branched chain unsaturated acyclichydrocarbons such as 3,4-dipropyl-1,3-hexadien-5-yne,5,5-dimethyl-1-hexene, and the like; cyclic hydrocarbons, saturated orunsaturated, such as cyclohexane, decahydronaphthalene,tetrahydronaphthalene, 2-methyl naphthalene, and the like; and includingsuch aromatics as cumene, mesitylene, styrene, toluene, o-xylene, or thelike. The more preferred hydrocarbons are those derived from petroleum,including especially admixtures of petroleum hydrocarbons characterizedin virgin naphthas, cracked naphthas, Fischer-Tropsch naphtha, light catcycle oil, heavy cat cycle oil, and the like, typically those containingfrom about 5 to about 30 carbon atoms, preferably from about 5 to about20 carbon atoms and boiling within a range of from about 30° C. to about450° C., preferably from about 150° C. to about 300° C.

The sulfur, or sulfur-bearing compound is characterized as anorgano-sulfur, or hydrocarbyl-sulfur compound which contains one or morecarbon-sulfur bonds within the total molecule, and generally includesacyclic or cyclic, saturated or unsaturated, unsubstituted or inertlysubstituted compounds. Exemplary of acyclic compounds of this characterare ethyl sulfide, n-butyl sulfide, n-hexyl thioalcohol, dimethyldisulfide, dimethyl sulfone, dimethyl sulfoxide, and the like; cycliccompounds of such character are methylthiobenzene, methyl dithiobenzene,thiophene, benzothiophene, 5-formamido-benzothiozole,1-naphthalenesulfonic acid, dibenzylthiophene, and the like. Suitably,the sulfur concentration of the feed ranges from about 0.01 percent toabout 10 percent, preferably from about 0.1 to about 2 percent, based onthe total weight of the feed. Suitably, both the hydrocarbon and sulfurfor the reaction can be supplied by the use of a heterocyclic sulfurcompound, or compounds. Exemplary of heterocyclic sulfur compoundssuitable for such purpose are thiophene, dibenzothiophene,tetraphenylthiophene, tetramethyldibenzothiophene,tetrahydrodibenzothiophene, thianthrene, titramethylthianthrene, and thelike. The hydrogen required for forming the catalysts of this inventionmay be pure hydrogen, an admixture of gases rich in hydrogen or acompound which will generate in situ hydrogen, e.g., a hydrogen-bearinggas such as hydrogen sulfide, or a hydrogen donor solvent.

In decomposing the catalyst precursor, a bed of the dried catalystprecursor is contacted in a hydrogen atmosphere with the hydrocarbon andsulfur, or sulfur-bearing compound, and heated at conditions whichdecompose the diammonium ion substituted, ammonium or quaternaryammonium ion substituted, or ionic form of a basic cyclic aminesubstituted thiomolybdate, or thiotungstate, salt component of saidcatalyst precursor. For example, a fixed bed of the dried catalystprecursor is charged into a reaction vessel and contacted with a liquidhydrocarbon, or admixture of liquid hydrocarbons, generally at a flowrate of hydrocarbon:catalyst precursor of from about 0.05 to about 50,preferably from about 0.1 to about 10, volumes of hydrocarbon per volumeof catalyst per hour, a flow rate of hydrogen ranging from about 250 toabout 5000 SCF/Bbl, preferably from about 500 to about 3000 SCF/Bbl, andat pressures ranging from about 50 to about 4000 pounds per square inchgauge (psig), preferably 150 to about 2500 psig. Typically thehydrocarbon is introduced downflow, but can be introduced upflow ordownflow over the bed of catalyst precursor, with the organo, orhydrocarbyl sulfur compound being added to the hydrocarbon feed. Theorgano, or hydrocarbyl sulfur compound is added in sufficient quantityto the feed such that the sulfur content of the feed ranges from about0.1 percent to about 10 percent, preferably from about 0.5 percent toabout 3 percent, calculated as elemental sulfur based on the weight ofthe hydrocarbon feed. The temperature of the reaction is graduallyraised until the decomposition temperature of the organo or hydrocarbyldiammonium ion substituted, ammonium or quaternary ammonium ionsubstituted, or ionic form of a basic cyclic amine substitutedthiomolybdate, or thiotungstate, salt component is reached, at whichtime the temperature is held substantially constant until thedecomposition reaction is completed. Typically the decompositiontemperature of the organo or hydrocarbyl diammonium ion substituted,ammonium or quaternary ammonium ion substituted, or ionic form of abasic cyclic amine substituted thiomolybdate, or thiotungstate, saltdecomposes generally at peak operating temperatures ranging betweenabout 150° C. and 400° C., more often between about 200° C. and 370° C.

In the preparation of the catalysts of this invention, the salts of thecatalyst precursor composite are decomposed in an atmosphere ofhydrogen, and in the presence of hydrocarbon and sulfur; the latterspecies of which can be provided by a sulfur-containing hydrocarbonspecies, or separately by a hydrocarbon compound, or compounds, andsulfur or a sulfur-containing compound, or compounds. The salts of thecatalyst precursor composite decompose at temperatures ranging betweenabout 150° C. and 400° C., and more generally between about 200° C. and350° C. which temperatures correspond generally with, or are exceeded byhydrotreating temperatures. Where, however, the decompositiontemperature of the catalyst precursor is lower than the desiredhydrotreating temperature, the temperature in conducting thehydrotreating process is raised to that which is desired for conductingthe hydrotreating operation. In a typical operation, hydrotreatingconditions are provided as regards hydrogen pressures, space velocitiesand hydrogen gas recycle rates, and the temperature is gradually raisedto the decomposition temperature of the catalyst precursor, the catalystprecursor is decomposed in the presence of the hydrogen, hydrocarbon andsulfur to form the catalytically active species, and the temperaturethen further increased as desired to conduct the hydrotreatingoperation. Hydrotreating conditions vary considerably depending on thenature of the hydrocarbon being hydrogenated, the nature of theimpurities or contaminants to be reacted or removed, and, inter alia,the extent of conversion desired, if any. In general however, thefollowing are typical conditions for hydrotreating a naphtha boilingwithin a range of from about 25° C. to about 210° C., a diesel fuelboiling within a range of from about 170° C. to 350° C., a heavy gas oilboiling within a range of from about 325° C. to about 475° C., orresiduum containing from about 10 percent to about 50 percent of amaterial boiling above about 575° C.

    ______________________________________                                                              Pres-   Space  Hydrogen                                              Temp.,   sure    Velocity                                                                             Gas Rate                                 Feed         °C.                                                                             psig    V/V/Hr SCF/B                                    ______________________________________                                        Naptha  Typical  100-370  150-  0.5-10  100-2000                                                        800                                                         Preferred                                                                              150-260  250-    2-6   500-1500                                                        400                                                 Diesel  Typical  200-400  250-  0.5-4   500-6000                              Fuel                      1500                                                        Preferred                                                                              260-340  400-    1-2  1000-2000                                                        1000                                                Heavy   Typical  260-430  250-  0.3-2  1000-6000                              Gas Oil                   2500                                                        Preferred                                                                              320-385  600-  0.5-1  1500-4000                                                        1250                                                Residuum                                                                              Typical  340-450  1000- 0.1-1  2000-10,000                                                      5000                                                        Preferred                                                                              360-400  1250-  0.25-0.5                                                                            4000-6000                                                        2000                                                ______________________________________                                    

The catalyst of this invention can be promoted to further dramaticallyincrease the activity of the finished catalyst by the further additionof a Group VIII metal of the Periodic Table of the Elements (E. H.Sargent & Co., Copyright 1962, Dyna-Slide Co.), which metal can be addedto the refractory porous inorganic oxide, or alumina, support prior to,simultaneously with, or subsequent to the decomposition of the organo orhydrocarbyl diammonium ion substituted, ammonium or quaternary ammoniumion substituted, or ionic form of a basic cyclic amine substitutedthiomolybdate, or thiotungstate, salt on treatment of the catalystprecursor in the presence of hydrogen, hydrocarbon, and sulfurcomponents. Suitably such metal promoter, or metal promoters,particularly iron, cobalt and nickel, alone or in admixture one metalwith another, is incorporated with the support, notably alumina, as viacogellation or impregnation prior to incorporation of the organo orhydrocarbyl diammonium ion substituted, ammonium or quaternary ammoniumion substituted, or ionic form of a basic cyclic amine substitutedthiomolybdate, or thiotungstate, salt with the dried, calcined support.Preferably, the metal promoter, or metal promoters, is added to thecatalyst after the organo or hydrocarbyl diammonium ion substituted,ammonium or quaternary ammonium ion substituted, or ionic form of abasic cyclic amine substituted thiomolybdate, or thiotungstate, saltimpregnated upon the support has been treated, and decomposed.

The Group VIII metal components, admixed one component with another orwith a third or greater number of metal components, can be composited orintimately associated with the porous inorganic oxide support byimpregnation of the support with metals, e.g., with the alumina, by an"incipient wetness" technique, or technique wherein a metal, or metalsis contained in a solution, preferably water, alcohol, or ketone inmeasured amount and the entire solution is absorbed into the support andsubsequently dried, and calcined if desired, to form the catalyst. Thevolume amount of solution to be employed in such recipe is separatelydetermined by measuring the amount of solvent required to wet a knownweight of support to the point where some liquid bridging betweenparticles or some miniscus formation between particles and containerwalls just becomes evident. This ratio of volume of solution to weightof support is then used proportionally to calculate the volume ofsolution containing catalytic metals to be used in the incipient wetnessimpregnation. Impregnation by adsorption of the metals from dilutesolution onto the support can also be used but this method is moreappropriate for low concentrations, e.g., from about 0.01 to about 1.0percent of catalytic metals desired, and it is less preferable for usein the higher metals concentration ranges. The metal impregnatedsupport, after impregnation, is dried, e.g., at temperatures rangingfrom about 20° C. to about 150° C., preferably at ambient temperatures,e.g., from about 20° to about 30° C., until free flowing and then fromabout 80° C. to about 110° C. as in a circulating air, vacuum oven,microwave oven, or the like.

The following examples, with comparative demonstrations, are furtherexemplary of the highly active, highly selective catalysts of thisinvention for use in hydrotreating, especially hydrodesulfurization(HDS) or hydrodenitrogenation (HDN), or both. In the examples anddemonstrations which follow, all parts are in terms of weight units,pressures in terms of pounds per square inch gauge, temperatures areexpressed in terms of degrees Centigrade, gas flow rates in terms ofSCF/Bbl, and liquid flow rates in terms of LHSV except as otherwisespecified.

EXAMPLE 1

This example demonstrates the advantages of catalysts prepared by theprocess of this invention, i.e., by decomposing the supported complexsalt, B_(x) [MO_(y) S_(4-y) ], in the presence of hydrogen, hydrocarbonand sulfur to produce a catalyst of high hydrodesulfurization activity,and high hydrodenitrogenation activity. The hydrodesulfurization andhydrodenitrogenation activity of this catalyst is compared with oneproduced according to the method disclosed and claimed in our copendingapplication Ser. No. 400,005, filed of even date herewith, and with acommercially available hydrodesulfurization catalyst.

A solution was prepared by dissolving 38.628 g of tetrabutylammoniumthiomolybdate in enough methanol to give 80 ml of solution. Analysis ofthe tetrabutylammonium thiomolybdate indicated that it had theapproximate formula ((C₄ H₉)₄ N)₂ (MoO₀.2 S₃.8).1.7H₂ O. A 50 ml portionof this solution was used to impregnate to incipient wetness 50 g ofgamma alumina, which had 265.7 m² /g surface area and 0.750 ml/g porevolume, and which had been gound and screened to 14/35 Tyler mesh andcalcined 4 hours at 540° C. before impregnation. The alumina was driedovernight in a vacuum desiccator, then impregnated with the remaining 30ml of solution and dried for 5 hours in a vacuum desiccator. The 88.3 gof impregnated alumina so prepared contained 13.29 weight percent MoO₃on an ignition-loss free basis (ignition loss=38.6%).

Two catalysts, designated A and B, were prepared from this same batch ofimpregnated alumina. Catalyst A, the catalyst of this invention, wasprepared by decomposing the catalyst precursor composite in anatmosphere of hydrogen, hydrocarbon and sulfur whereas Catalyst B wasprepared by decomposing the catalyst precursor composite in the presenceof hydrogen and hydrogen sulfide, as disclosed and claimed inapplication Ser. No. 400,005, supra.

In the preparation of catalyst A, the catalyst of this invention, 28.0 g(35 ml) of the impregnated alumina was thermally decomposed in a fixedbed reactor by (1) heating under 500 psig of H₂ to 200° C., (2)establishing a liquid feed flow of 0.825 LHSV with a blend of 5%dibenzothiophene (DBT) dissolved in decalin and a gas flow of 900 SCF/Bwith 100% H₂, still at 500 psig, (3) holding 4.5 hours at 200° C., andthen (4) heating to 330° C. and holding for 16 hours. The reactor wascooled under hydrogen and discharged in an inert atmosphere, yielding19.77 g of solids material. The solids material was promoted byimpregnating in an inert atmosphere with 2.54 g of cobalt nitrate,dissolved in enough acetone to give 16 ml of solution, and dryingovernight in a vacuum desiccator. The finished Catalyst A contained 3.73weight percent CoO and 14.01 weight percent MoO₃, on an ignition-lossfree basis (ignition loss=19.5%), and had 183 m² /g surface area and0.425 ml/g pore volume.

In the preparation of Catalyst B, 24.2 g (30 ml) of the impregnatedalumina was thermally decomposed in a fixed bed reactor by (1)establishing a flow of 15.0 std liters/hr of nitrogen at roomtemperature and atmospheric pressure, (2) heating to 200° C., (3)switching to a flow of 15.0 std liters/hr of 10 vol.% hydrogen sulfidein hydrogen, at atmospheric pressure, (4) holding at 200° C. for 2hours, and the (5) heating to 327° C. and hold for 16 hours. The reactorwas cooled under nitrogen and discharged in an inert atmosphere yielding17.6 g of solids material. The solids material was promoted byimpregnating in an inert atmosphere with 2.18 g of cobalt nitrate,dissolved in enough acetone to give 14 ml of solution, and dryingovernight in a vacuum desiccator. The finished Catalyst B contained 4.24weight percent CoO and 13.63 weight percent MoO₃, on an ignition-lossfree basis (ignition loss=15.8%). The catalyst also contained 2.31 wt. %carbon and 5.70 wt. % sulfur, and had 188 m² /g surface area and 0.492ml/g pore volume.

The catalytic activity of Catalyst A and B were measured in aside-by-side hydrotreating test, along with a conventional, commerciallyavailable cobalt molybdenum catalyst. The conventional catalystcontained 3.22 weight percent CoO and 12.81 weight percent MoO₃, and had239 m² /g surface area and 0.471 ml/g pore volume. The test feedstockwas a Baton Rouge light catalytic cycle oil (LCCO) designated FS-4754.Inspections on this feedstock are given in Table I.

                  TABLE I                                                         ______________________________________                                        Feedstock Inspections                                                         Feedstock No.     FS-4754  FS-5171                                            ______________________________________                                        API Gravity       19.3     15.6                                               Sulfur, Wt. %     1.48     1.74                                               Nitrogen, ppm     327      274                                                Bromine No. mg/cc 4.4      5.6                                                Carbon, wt. %     88.51    88.81                                              Hydrogen, wt. %   9.98     9.42                                               FIA Aromatics     71.0                                                        Olefins           2.5                                                         Saturates         27.0                                                        Distillation                                                                  5%                473      465                                                50%               538      516                                                95%               634      642                                                ______________________________________                                    

Hydrotreating conditions were 330° C., 750 psig, and 1200 SCF/B of 100%H₂ with space velocities ranging from 0.5 to 2.0 V/H/V. Activity wasmeasured as the reciprocal space velocity required to reach a givendesulfurization or denitrogenation target, and relative activitiesremained constant over the entire range of 85-97% HDS and 62-98% HDN.Per gram of molybdenum, Catalyst A had 1.47 times the desulfurizationactivity and 1.81 times the denitrogenation activity of the conventionalcatalyst. Catalyst B had only 0.79 times the desulfurization activity ofthe conventional catalyst, but had 1.70 times the denitrogenationactivity. Thus Catalyst A has much higher HDS activity than eithercatalyst B or the conventional catalyst (Catalyst B, on the other hand,has a much higher HDN/HDS selectivity.)

These data clearly demonstrate the advantage of carrying out thedecomposition of the catalyst precursor composite in the presence of ahydrocarbon and a sulfur-bearing compound, when high HDS activity isdesired. It also demonstrates the difrerence between the catalysts ofthis invention and otherwise similar but unsupported catalysts ofPecoraro and Chianelli, or Chianelli and Pecoraro, supra, because of theselectivity in the preparation of the catalysts.

EXAMPLE 2

This example demonstrates that a superior catalyst can be prepared fromdiamines, such as ethylenediamine.

A solution was prepared by dissolving 31.40 g of an ethylenediamine saltof thiomolybdic acid in 70.00 g of ethylenediamine. Analysis of the saltindicated that only one nitrogen of each ethylenediamine moiety wasprotonated, and that the anion was almost completely sulfided, so thatthe salt had the approximate formula (H₂ NC₂ H₄ NH₃)₂ (MoS₄). To thissolution, an 83.5 g portion of the same 14/35 mesh calcined gammaalumina used in Example 1 was slowly added. The mixture was stirredduring the alumina addition and for an additional 30 minutes. Excessethylenediamine was removed by vacuum distillation at 30° C. for 48hours.

Of the 128.9 g of impregnated alumina so prepared, 29.1 g (35 ml) wasthermally decomposed in a fixed bed reactor under the same conditions asemployed in Example 1 for the preparation of Catalyst A. The reactor wascooled under hydrogen and discharged in an inert atmosphere, yielding24.96 g of solids material. The solid material was promoted byimpregnating in an inert atmosphere with 2.54 g of cobalt nitrate,dissolved in eough acetone to give 16 ml of solution, and dryingovernight in a vacuum desiccator. The finished catalyst, designated C,contains 3.55 weight percent CoO and 14.28 weight percent MoO₃, on aignition-loss free basis (ignition loss=18.46%). It also contained 5.53wt. % carbon and 5.52 wt. % sulfur, and had 207 m² /g surface area and0.492 ml/g pore volume.

The catalytic activity was measured in the same way as for Example 1,except that the hydrogen treat gas rate was increased to 1500 SCF/B.Compared to the same conventional catalyst, this catalyst had 1.28 timesthe desulfurization activity and 1.88 times the denitrogenationactivity, per gram of molybdenum.

EXAMPLE 3

A solution was prepared by dissolving 64.0 g of tetrabutylammoniumthiomolybdate in enough methanol to give 160 ml of solution. Analysis ofthe tetrabutylammonium thiomolybdate indicated that it had theapproximate formula ((C₄ H₉)₄ N)₂ (MoO₀.4 S₃.6).H₂ O. A 90 ml portion ofthis solution was used to impregnate to incipient wetness 83.5 g of thesame 14/35 mesh calcined gamma alumina used in Example 1. The aluminawas dried overnight in a vacuum desiccator, then impregnated with theremaining 70 ml of solution and dried for 3 days in a vacuum desiccator.

Of the 142.64 g of impregnated alumina so prepared, 23.2 g (30 ml) wasthermally decomposed in a fixed bed reactor by (1) establishing a liquidfeed flow of 1.0 LHSV with a blend of 5% DBT dissolved in decalin and agas flow of 900 SCF/B with 100% H₂, at room temperature and 500 psig,(2) heating to 200° C. at 2.5 °/min, (3) holding at 200° C. for 2 hours,(4) heating to 330° C. at about 2 °/min, and (5) holding at 330° C. for16 hours. The reactor was hydrogen-stripped at atmospheric pressure for30 minutes, cooled under hydrogen, and discharged in an inertatmosphere, yielding 17.0 g of solids material. Of this material, 16.0 gwas promoted by impregnating in an inert atmosphere with 2.30 g ofcobalt acetate, dissolved in enough methanol to give 15 ml of solution,and drying overnight in a vacuum desiccator. The finished catalyst,which is designated D, contained 3.30 weight percent CoO and 12.23weight percent MoO₃, on an ingition-loss free basis (ignitionloss=13.26%). Catalyst D also contained 5.17 wt. % carbon and 4.33 wt. %sulfur, and had 202 m² /g surface area and 0.446 ml/g pore volume.

The catalytic activity of Catalyst D was measured in the same way as forExample 1, except that the hydrogen treat gas rate was increased to 1500SCF/B and the temperature was reduced to 325° C. Catalyst D, with theslightly different decomposition conditions and promoted with cobaltacetate instead of cobalt nitrate, it will be observed was even moreactive than Catalyst A. It had 2.01 times the desulfurization activityof the conventional catalyst, and 2.40 times the denitrogenationactivity, per gram of molybdenum.

The hydrogen content of the feed, liquid product, and off-gas were verycarefully measured, and the chemical hydrogen consumption of Catalyst Dand the commercial catalyst were determined. Chemical hydrogenconsumption is thus usually very closely correlated with nitrogenremoval, since carbon-nitrogen bonds are stabilized by adjacent aromaticring structures and are usually broken only after such aromatic ringshave been hydrogenated. It was found that the relationship is morefavorable for the catalysts of this invention than for the conventionalcatalysts. Hydrotreating to 80 ppm nitrogen in the liquid product,Catalyst D thus required only 625 SCF/B hydrogen consumption, while theconventional catalyst required 750 SCF/B. Hydrotreating to 20 ppmnitrogen, the chemical hydrogen consumptions were 725 and 850 SCF/B,respectively. A second conventional catalyst was later tested to checkthis result, the second conventional catalyst containing higher levelsof CoO and MoO₃, i.e., 4.08 wt. % and 15.86 wt. %, respectively; and ithad 235 m² /g surface area and 0.480 ml/g pore volume. In spite of thedifference in catalytic metals levels, at any given product nitrogenlevel the hydrogen consumption over the second conventional catalyst wasindistinguishable from the consumption over the first conventionalcatalyst. The accuracy of determination of the hydrogen consumptionvalues is about 30 SCF/B. Thus, the catalyst of this invention canhydrotreat to a given nitrogen target with about a 125 SCF/B savings inhydrogen consumption, this representing considerable cost savings.

EXAMPLE 4

Nickel promoted versions of the catalyst of this invention, Catalysts Eand F, were made as follows: A solution was prepared by dissolving 72.0g of tetrabutylammonium thiomolybdate in enough methanol to give 180 mlof solution. Analysis of the tetrabutylammonium thiomolybdate indicatedthat it had the approximate formula ((C₄ H₉)₄ N)₂ (MoO₀.5 S₃.5). Thissolution was used to impregnate to incipient wetness a 167.0 g portionof the same 14/35 mesh calcined gamma alumina used in Example 1. Thealumina was dried for 3 days in a vacuum desiccator. It was thenimpregnated with a second solution of 56.0 g of tetrabutylammoniumthiomolybdate, having essentially the same analyses, dissolved in enoughmethanol to give 140 ml of solution, and dried in a vacuum desiccatorovernight. The 295.8 g of impregnated alumina so prepared contained13.96 weight percent MoO₃, on an ignition-loss free basis (ignitionloss=36.43%).

Two portions of this impregnated alumina, with a combined weight 79.5 g(96 ml) were thermally decomposed in fixed bed reactors at the sameconditions described in Example 3. They were discharged in an inertatmosphere and recombined, yielding 54.2 g of material.

Of this thermally decomposed sample, 25.2 g was impregnated with 2.43 gof nickel acetate dissolved in enough methanol to make 22 ml ofsolution. This material was dried in a vacuum desiccator overnight togive Catalyst E. The finished catalyst contained 2.20 weight percentelemental Ni and 12.00 weight percent MoO₃, on an ignition-loss freebasis (ignition loss=11.40%). It also contained 3.3 wt. % carbon and anundetermined amount of sulfur.

Another 25.2 g of the thermal decomposed sample was impregnated with2.84 g of nickel nitrate, also dissolved in enough methanol to make 22ml of solution. This material was dried in a vacuum desiccator overnightto give Catalyst F. The finished catalyst analyzed 2.30 weight percentNi and 12.20 weight percent MoO₃, on an ignition-loss free basis(ignition loss=12.72%). It also contained 1.90 wt. % carbon.

The catalytic activity of these catalysts were measured in the same wayas was the catalyst in Example 3. As is typical for Ni/Mo catalysts, thedesulfurization activities were somewhat lower than that of the Co/Moconventional catalyst, by a factor of 0.72 for Catalyst E and 0.62 forCatalyst F, per gram of molybdenum. However, the denitrogenationactivities were quite high, 1.92 times and 1.91 times the activity ofthe conventional catalyst, for Catalyst E and F. respectively.

EXAMPLE 5

In this example, addition of the promoter compound was performed beforethermal decomposition of the amine thiomolybdate compound.

A solution was prepared by dissolving 64.0 g of a typicaltetrabutylammonium thiomolybdate prep in enough methanol to give 160 mlof solution. A 90 ml portion of this solution was used to impregnate toincipient wetness 83.5 g of a portion of the same 14/35 mesh calcinedgamma alumina used in Example 1. The alumina was dried overnight in avacuum desiccator, then impregnated with the remaining 70 ml of solutionand dried overnight in a vacuum desiccator. The impregnated alumina wasthen further impregnated, without any intervening treatment, with asolution consisting of 11.63 g of cobalt acetate dissolved in enoughmethanol to give 70 ml of solution, and dried for 4 days in a vacuumdesiccator. The 159.9 g specimen of catalyst precursor so prepared isdesignated Catalyst G. The specimen contained 3.32 weight percent CoOand 13.73 weight percent MoO₃, on an ignition-loss free basis (ignitionloss=37.11%). It also contained 20.55 wt. % carbon and an undeterminedamount of sulfur.

This specimen was thermally decomposed in the same fixed bed reactor inwhich the activity test was carried out. Prior to the activity test, aliquid feed flow of 1.0 LHSV with a blend of 5% DBT dissolved in decalinand a gas flow of 900 SCF/B with 100% H₂ were established at roomtemperature and 500 psig. The temperature was increased to 200° C., heldthere for 2 hours, increased to 330° C., and held there for 16 hours.The DBT/decalin blend flow was discontinued, the reactor cooled to 325°C., pressure increased to 750 psig, and the flow rates for LCCO andhydrogen were established for the activity test. Catalyst G had 0.78times the desulfurization activity of the conventional catalyst, and1.69 times the denitrogenation activity, per gram of molybdenum.

EXAMPLE 6

This example is designed to distinguish between the catalysts of thepresent invention, and catalysts disclosed in U.S. Pat. No. 4,243,553,supra, obtained by thermally decomposing selected thiomolybdate salts inthe presence of essentially inert, oxygen-free atmospheres.

Four catalysts, designated H, J, K, and L, were prepared. Thepreparation of Catalyst H used both thermal decomposition in thepresence of a hydrocarbon and a sulfur-bearing compound, in accordancewith the present invention, and including promotion with cobalt afterdecomposition, according to a preferred embodiment of the presentinvention. The preparation of Catalyst J used the thermal decompositionof this invention, combined with a promotion technique which wasdisclosed in U.S. Pat. No. 4,243,553, but would be within the scope ofthe current invention. The preparation of Catalyst K followed theteachings of U.S. Pat. No. 4,243,553 as regards both promotion anddecomposition. The fourth preparation, Catalyst L, was decomposed in aninert atmosphere, according to the teachings of U.S. Pat. No. 4,243,553,but promoted after decomposition, according to the preferred embodimentof the current invention.

Preparation of catalysts: Specifically, two preparations oftetrabutylammonium thiomolybdate supported on alumina were made exactlyas in Example 5, except as regards the specific physical properties ofthe alumina, and then combined in a masterbatch to give 309.19 g ofimpregnated alumina. This alumina had 255.1 m² /g surface area and 0.684ml/g pore volume, and was also ground and screened to 14/35 Tyler mesh,then calcined 4 hours at 540° C. before impregnation.

Preparation of Catalyst H: Two portions of this impregnated alumina fromthe masterbatch, with a combined weight of 73.5 g (88 ml), was thermallydecomposed in fixed bed reactors at the same conditions described inExample 3. The reactors were discharged in an inert atmosphere and thealumina portions recombined, yielding 47.3 g of solids material. Of thismaterial, 31.66 g was impregnated with a solution of 3.48 g of cobaltacetate dissolved in enough methanol to make 31 ml of solution. This wasdried in a vacuum deiccator for 3 days, to provide Catalyst H.

Preparation of Catalyst J: A larger portion of the impregnated aluminafrom the masterbatch, 149.9 g was impregnated with 16.49 g of cobaltacetate dissolved in enough water to make 150 ml of solution. Whilestill wet, the alumina was treated in a packed bed with a flow of 100ml/min of 100% hydrogen sulfide for 1.5 hours, then flushed withnitrogen for 10 minutes. The alumina was dried in a vacuum desiccatorfor 17 days. Half of this alumina was thermally decomposed in fixed bedreactors at the same conditions described in Example 3, yielding 50.9 gof Catalyst J.

Preparation of Catalyst K: The other half of the specimen left over fromthe preparation of Catalyst J was placed in a fixed bed at atmosphericpressure, with a flow of 50 std liters/hour of nitrogen. It was heatedat a rate of 1.5 deg/min to 450° C., held at 450° C. for 2 hours, andcooled under nitrogen. The sample was treated with 25 std liters/hour of2% oxygen in nitrogen for 1 hour at room temperature, to prevent it frombeing pyrophoric, and then discharged, yielding 54.1 g of Catalyst K.

Preparation of Catalyst L: A third portion of the original impregnatedalumina from the masterbatch, 74.9 g was decomposed under nitrogen atthe described conditions, yielding 48.2 g of solids material. Of this,32.3 g was impregnated with a solution of 3.55 g of cobalt acetate, anddissolved in enough methanol to give 32 ml. of solution. This materialwas dried in a vacuum desiccator overnight, yielding 36.8 g of CatalystL.

All four catalysts were tested for catalytic activity in identicalside-by-side fixed-bed reactors. No conventional catalyst was includedin this test, and the activities are expressed as absolute volumetricrate constants, rather than relative to a standard. The kinetic rateconstants are shown in Table II for hydrotreating feedstock FS-4754(Table I) at 325° C., 750 psig, and 1500 SCF/B, with space velocitiesranging from 0.5 to 2.0 V/H/V.

                  TABLE II                                                        ______________________________________                                        Catalyst Activities After Decomposition Under                                 Inert or Reducing, Sulfur-Bearing Conditions                                                                 Sulfur Nitrogen                                                               Removal                                                                              Removal                                                                Rate   Rate                                    Catalyst                                                                              Decomposition                                                                             Promotion  Constant                                                                             Constant                                ______________________________________                                        H       Red/Sulf    After      0.89/Hr                                                                              1.94/Hr                                 J       Red/Sulf    Before     0.36   1.38                                    K       Inert       Before     0.36   0.50                                    L       Inert       After      0.71   0.90                                    ______________________________________                                    

These data show that Catalyst H, prepared according to a preferredembodiment of this invention, was far more active for both sulfur andnitrogen removal than Catalyst K, made according to the teachings ofU.S. Pat. No. 4,243,553, or Catalyst L, also covered by that patent.Catalyst J, a less preferred embodiment, is not as active, but isclearly a different material from Catalyst K or L, as demonstrated byits unusually high HDN/HDS selectivity 1.38/0.36.

The aforementioned U.S. Patent discloses the use of materials such asCatalyst K in hydrotreating, but it is principally concerned with theuse of unpromoted versions in methanation. Therefore, samples ofCatalyst H and L, before these materials were promoted, were tested formethanation activity. The test was carried out at 400° C., 400 psig,GHSV=3000, using a feed with H₂ /CO=3. After 1 hour, the unpromotedversion of catalyst H gave 40% conversion of CO to hydrocarbons, whilethe unpromoted version of Catalyst L gave only 35%. After 20 hours, theconversions were 33% and 29%, respectively. Thus, decomposition of asupported amine thiomolybdate salt in the presence of a hydrocarbon anda sulfur-bearing compound gives a superior catalytic material thandecomposition in an inert atmosphere, for methanation as well as forhydrotreating.

EXAMPLE 7

The catalysts of this invention described in previous examples all havemolybdenum contents corresponding to an equivalent MoO₃ content in therange of 12-14 wt. %, which is very close to the MoO₃ content of theconventional catalyst to which they have been compared. However, somecommercial catalysts of more recent vintage have higher loadings, often14-16 wt. % MoO₃, and sometimes even up to 20 wt. %. Accordingly, thecatalyst described in the folowing example, was prepared with a highermolybdenum content, and a catalyst made in accordance with thisinvention is compared to such commercial catalyst, specifically thesecond conventional catalyst described in Example 3, containing 4.08 wt.% CoO and 15.86 wt. % MoO₃, and having 235 m² /g surface area and 0.480ml/g pore volume.

Preparation of Catalyst M: To make Catalyst M, a solution was preparedby dissolving 84.0 g of tetrabutylammonium thiomolybdate in enoughmethanol to give 150 ml of solution. Analysis of the tetrabutylammoniumthiomolybdate indicated that it had the approximate formula ((C₄ H₉)₄N)₂ (MoO₀.8 S₃.2). An 85 ml portion of this solution was used toimpregnate 78.5 g of the same calcined 14/35 mesh gamma alumina as usedin Example 6. The alumina was dried overnight in a vacuum desiccator,then impregnated with the remaining 65 ml of solution and again driedovernight in a vacuum desiccator.

Of the 160.0 g of impregnated alumina so prepared, three portions, eachweighing 46.4-46.6 g (60 ml), were thermally decomposed in fixed bedreactors at the same conditions described in Example 3. Each wasdischarged in an inert atmosphere, yielding 28.0-28.2 g of material, andwas separately impregnated with a solution of 4.35 g of cobalt acetatedissolved in enough methanol to make 28.0 ml of solution, then dried ina vacuum desiccator for three days. The three portions were re-combinedto make Catalyst M, with a total yield of 96.99 g. Catalyst M contained4.64 wt. % CoO and 14.97 wt. % MoO₃, on an ignition-loss free basis(ignition loss=10.35%). The catalyst also contained 6.43 wt. % carbonand 5.13 wt. % sulfur, and had 225 m² /g surface area and 0.410 ml/gpore volume.

The catalytic activity of Catalyst M and the second conventionalcatalyst were determined side-by-side in the same manner described inExample 3. Catalyst M had 1.38 times the desulfurization activity and1.94 times the denitrogenation activity, per gram of molybdenum.

EXAMPLE 8

Many of the amine thiomolybdate salts, including tetrabutylammoniumthiomolybdate, will melt at a lower temperature than their decompositiontemperature. This is desirable, because it allows the salt to wet theporous support and become more highly dispersed as it is being heatedfor decomposition. It is also desirable because it makes possible thepreparation of impregnated materials without any added solvent, as shownin this example.

A mixture was made of 60.13 g of tetrabutylammonium thiomolybdate and67.69 g of the same 14/35 mesh calcined gamma alumina described inExample 6. Analysis of the tetrabutylammonium thiomolybdate indicatedthat it had the approximate formula ((C₄ H₉)₄ N)₂ (MoO₀.2 S₃.8). Themixture was heated and stirred in a Rotovap under a nitrogen blanket for2 hours at 130° C., then for 2 hours at 180° C., during which time thetetrabutylammonium thiomolybdate melted and impregnated the aluminawithout any added solvent. This procedure yielded 114.40 g ofimpregnated alumina which analyzed 16.43 wt. % MoO₃ on an ignition-lossfree basis (ignition loss=30.54%). It also contained 19.99 wt. % carbonand 7.57 wt. % sulfur.

Three portions of this impregnated alumina, with a combined weight of109.36 g (105 ml), were thermally decomposed in fixed bed reactors atthe same conditions described in Example 3. The specimens weredischarged in an inert atmosphere and recombined, yielding 76.93 g ofmaterial.

Of this thermally decomposed sample, 38.43 g was impregnated with 4.71 gof cobalt acetate, dissolved in enough methanol to make 38 ml ofsolution. This material was dried in a vacuum desiccator overnight togive Catalyst N. The finished catalyst contained 4.19 wt. % CoO and15.76 wt. % MoO₃, on an ignition-loss free basis (ignition loss=7.26%).It also contained 5.22 wt. % carbon and 6.30 wt. % sulfur, and had 220m² /g surface area and 0.411 ml/g pore volume.

The catalytic activity was measured in the same way as for Example 7,except that a different LCCO feedstock, designated FS-5171, was used.Inspections on this feedstock are listed in Table I. It was found thatit makes very little difference whether the tetrabutylammoniumthiomolybdate is impregnated onto the alumina from methanol solution orfrom the thiomolybdate melt. Catalyst N had 1.38 times thedesulfurization activity of the newer generation conventional catalyst,and 1.73 times the denitrogenation activity, per gram of molybdenum.

EXAMPLE 9

In Example 5, the catalyst was promoted before the amine thiomolybdatesalt was decomposed, and in all other preceding examples, after it wasdecomposed. In this example, a catalyst was prepared in which thepromoter was put onto the gamma alumina even before the aminethiomolybdate salt was impregnated.

Preparation of Catalyst O: A solution was prepared by dissolving 19.64 gof cobalt nitrate in enough water to give 75 ml of solution. Thissolution was used to impregnate 83.5 g of the 14/35 mesh calcined gammaalumina described in Example 6. The impregnated alumina was left coveredat room temperature overnight, then dried for 2 hours in an air oven at80° C. To more completely remove the water, at a low enough temperatureto avoid decomposition of the nitrate, the sample was subjected toazeotropic distillation with 250 ml of toluene at 110° C. for 4 hours,then dried overnight in a vacuum desiccator. Of the resulting 101.36 gof impregnated alumina, 67.69 g was mixed with 60.03 g oftetrabutylammonium thiomolybdate. Analysis of the tetrabutylammoniumthiomolybdate indicated that it had the approximate formula ((C₄ H₉)₄N)₂ (MoO₀.6 S₃.4). The mixture was heated and stirred in a Rotovap undera nitrogen blanket for 2 hours at 134° C., and then for 2 hours at 183°C., during which time the tetrabutylammonium thiomolybdate melted andimpregnated the alumina without any added solvent. Some sinteringoccurred, and the finished catalyst had to be broken up and re-screenedto 14/35 mesh. The finished catalyst, designated Catalyst O, contained4.25 wt. % CoO and 12.46 wt. % MoO₃, or an ignition-loss free basis(ignition loss=31.06%). The catalyst also contained 19.51 wt. % carbonand 7.44 wt. % sulfur, and had 108 m² /g surface area and 0.253 ml/gpore volume.

Catalyst O was thermally decomposed in the same fixed bed reactor inwhich the activity test was carried out. Prior to the activity test, aliquid feed flow of 1.0 LHSV with a blend of 5% DBT dissolved in decalinand a gas flow of 900 SCF/B with 100% H₂ were established at roomtemperature and 500 psig. The temperature was increased to 200° C., heldthere for 2 hours, increased to 330° C., and held there for 16 hours.The DBT/decalin blend flow was discontinued, the reactor cooled to 325°C., the pressure increased to 750 psig, and the flow rates for LCCO(FS-5171) and hydrogen were established for the activity test. Per gramof molybdenum, Catalyst O had somewhat low desulfurization activity,0.71 times that of the second conventional catalyst, but quite highdenitrogenation activity, 1.86 times that of the second conventionalcatalyst.

It is apparent that various modifications and changes can be madewithout departing the spirit and scope of the present invention.

Having described the invention, what is claimed is:
 1. A process for thepreparation of supported carbon-containing molybdenum sulfide andtungsten sulfide catalysts which comprisescompositing a preselectedquantity of a porous, refractory inorganic oxide with a saltcharacterized by the formula

    B.sub.x [MO.sub.y S.sub.4-y ]

where B is an organo or hydrocarbyl substituted diammonium ion, anorgano or hydrocarbyl substituted ammonium ion or quaternary ammoniumion, or an ionic form of a cyclic amine containing one or more basic Natoms, x is 1 where B is an organo or hydrocarbyl substituted diammoniumion, or 2 where B is an organo or hydrocarbyl substituted ammonium orquaternary ammonium ion or an ionic form of a cyclic amine containingone or more basic N atoms, M is molybdenum or tungsten, and y is 0, or afraction or whole number ranging up to 3, and heat decomposing the saltof said catalyst precursor composite in the presence of hydrogen,hydrocarbon and sulfur to form said supported carbon-containingmolybdenum sulfide or tungsten sulfide catalyst.
 2. The process of claim1 wherein the supported carbon-containing molybdenum or tungsten sulfidecatalyst precursor composite, prior to decomposition of the salt,contains from about 5 percent to about 30 percent of the salt,calculated as MoO₃ or WO₃ on an ignition loss free basis.
 3. The processof claim 1 wherein the catalyst precursor composite is heated attemperatures ranging from about 150° C. to about 400° C. to heatdecompose the salt of said composite.
 4. The process of claim 3 whereinthe decomposition temperature ranges from about 200° C. to about 370° C.5. The process of claim 1 wherein the decomposition temperature rangesfrom about 150° C. to about 400° C., the salt impregnated catalystprecursor composite is contacted with hydrogen at a flow rate rangingfrom about 250 to about 5000 SCF/Bbl, at pressures ranging from about 50to about 4000 psia, and with a liquid feed hydrocarbon at a flow rate ofhydrocarbon:catalyst precursor of from about 0.05 to about 50 volumes ofhydrocarbon per volume of catalyst per hour, and the added sulfur isequivalent to a sulfur content which ranges from about 0.1 to about 10percent, calculated as elemental sulfur based on the weight of thehydrocarbon feed.
 6. The process of claim 5 wherein the flow rate of thehydrogen ranges from about 500 to about 3000 SCF/Bbl, the pressureranges from about 150 to about 2500 psia, the flow rate of the liquidhydrocarbon ranges from about 0.1 to about 10, and the concentration ofsulfur ranges from about 0.5 percent to about 3 percent.
 7. The processof claim 1 wherein the porous, refractory inorganic oxide is alumina. 8.The process of claim 1 wherein the porous, refractory inorganic oxide isparticulate alumina, the salt is dissolved in a solvent, and theparticulate alumina and salt solution are contacted together and theparticulate alumina impregnated with the salt solution, the impregnatedalumina is dried to remove the solvent, and the dry, salt-impregnatedalumina heated to a temperature sufficient to decompose the salt andform said supported carbon-containing molybdenum sulfide or tungstensulfide catalysts.
 9. The process of claim 1 wherein, in the saltcharacterized by the formula B_(x) [MO_(y) S_(4-y) ], M is molybdenumand y ranges from 0 to 0.5.
 10. The process of claim 1 wherein a GroupVIII-B metal, or admixture of said metals, exclusive of said metal addedby incorporation of said heat decomposable thiomolybdate orthiotungstate salt, is composited with said supported carbon-containingmolybdenum sulfide or tungsten sulfide catalyst.
 11. As a composition ofmatter, supported carbon-containing molybdenum sulfide and tungstensulfide catalysts formed by the steps comprisingcompositing apreselected quantity of a porous, refractory inorganic oxide with a saltcharacterized by the formula

    B.sub.x [MO.sub.y S.sub.4-y ]

where B is an organo or hydrocarbyl substituted diammonium ion, anorgano or hydrocarbyl substituted ammonium ion or quaternary ammoniumion, or an ionic form of a cyclic amine containing one or more basic Natoms, x is 1 where B is an organo or hydrocarbyl substituted diammoniumion, or 2 where B is an organo or hydrocarbyl substituted ammonium orquaternary ammonium ion or an ionic form of a cyclic amine containingone or more basic N atoms, M is molybdenum or tungsten, and y is 0, or afraction or whole number ranging up to 3, and heat decomposing the saltof said catalyst precursor composite in the presence of hydrogen,hydrocarbon and sulfur to form said supported carbon-containingmolybdenum sulfide or tungsten sulfide catalyst.
 12. The composition ofclaim 11 wherein the supported carbon-containng molybdenum or tungstensulfide catalyst precursor composite, prior to decomposition of thesalt, contains from about 5 percent to about 30 percent of the salt,calculated as MoO₃ or WO₃ on an ignition loss free basis.
 13. Thecomposition of claim 11 wherein the catalyst precursor composite isheated at temperatures ranging from about 150° C. to about 400° C. toheat decompose the salt of said composite.
 14. The composition of claim13 wherein the decomposition temperature ranges from about 200° C. toabout 370° C.
 15. The composition of claim 11 wherein the decompositiontemperature ranges from about 150° C. to about 400° C., the saltimpregnated catalyst precursor composite is contacted with hydrogen at aflow rate ranging from about 250 to about 5000 SCF/Bbl, at pressuresranging from about 50 to about 4000 psia, and with a liquid feedhydrocarbon at a flow rate of hydrocarbon:catalyst precursor of fromabout 0.05 to about 50 volumes of hydrocarbon per volume of catalyst perhour, and the added sulfur is equivalent to a sulfur content whichranges from about 0.1 to about 10 percent, calculated as elementalsulfur based on the weight of the hydrocarbon feed.
 16. The compositionof claim 15 wherein the flow rate of the hydrogen ranges from about 500to about 3000 SCF/Bbl, the pressure ranges from about 150 to about 2500psia, the flow rate of the liquid hydrocarbon ranges from about 0.1 toabout 10, and the concentration of sulfur ranges from about 0.5 percentto about 3 percent.
 17. The composition of claim 11 wherein the porous,refractory inorganic oxide is alumina.
 18. The composition of claim 11wherein the porous, refractory inorganic oxide is particulate alumina,the salt is dissolved in a solvent, and the particulate alumina and saltsolution are contacted together and the particulate alumina impregnatedwith the salt solution, the impregnated alumina is dried to remove thesolvent, and the dry, salt-impregnated alumina heated to a temperaturesufficient to decompose the salt and form said supportedcarbon-containing molybdenum sulfide or tungsten sulfide catalysts. 19.The composition of clain 11 wherein, in the salt characterized by theformula B_(x) [MO_(y) S_(4-y) ], M is molybdenum and y ranges from 0 to0.5.
 20. The composition of claim 11 wherein a Group VIII-B metal, oradmixture of said metals, exclusive of said metal added by incorporationof said heat decomposable thiomolybdate or thiotungstate salt, iscomposited with said supported carbon-containing molybdenum sulfide ortungsten sulfide catalyst.